Methods of making flat sheet membrane element adapted for use in symbiotic fluids factionation, water treatment, and osmotic processes

ABSTRACT

The present application introduces design methodology and manufacturing procedures employing conventional permeable and semipermeable membrane flat sheet membrane apparatus [FSM], adapted for use in symbiotic fluids fractionation, water treatment, symbiotic osmotic processes of brine desalination and osmotic power generation, where flat sheet membranes are manufactured in the form of plurality of spaced apart, encaged self-supported unrolled membrane of flat surface panel (leaf) in three (3) categories, including; methodology for assembly of pre-cut flat sheet membrane panels, tube-like blown or rolled membrane film methodology, and blanketing membrane sheet methodology. Further assembling these flat sheet membranes in large membrane frames, where symbiotic reverse osmosis or symbiotic osmosis power generation membrane panels varies from about 250 mm (˜10 inch) to 1.00 m (˜40 inch) in width and 250 mm to 2.00 m (˜10-80 inch) in length or larger for a new unique approach in desalinating various water salinity sources. 
     Where, desalinated seawater recovery can exceed 85%, where water and chemicals can be recovered for reuse in Ecologically Sustainable Hydraulic Fracturing [ES-FRAC] processes of underground waters, and where generating osmotic power from brines can be achieved at 10-25 KW/liter-sec, depending on the source.

The inventor's U.S. Pat. Nos. 8,545,701, 8,852,432, 8,974,668, 9,156,003and PCT/IB2014/058861 are all deals with Induced Osmotic Potential [ISO]for salinity power generation employing hollow fiber membranes.

THE FIELD OF THE INVENTION

The current invention is intended to expand this field of technology byemploying conventional Flat Sheet Membranes not only in the broad fieldof symbiotically harnessing the potential of aqueous electrolyticsolutions by means of the natural phenomenon of osmosis, but also forfractionation of hydrocarbon and industrial gases, microfiltration,ultrafiltration and nanofiltration, as well as all processes that arebased on hollow fiber or spiral wound membranes. In essence, it is theinventor's attempt to standardize many of the technologies for molecularexchange or manipulation of fluids that are currently in use in water,solutions and gases technologies in just one adaptable technology.

Specifically, the invention introduces a unique process conceptapplicable in several processes including maximizing power generation,as in the case of Induced Symbiotic Osmosis [ISO] for salinity waterpower generation, seawater desalination recovery of 75% or higher,hypersaline water reverse osmosis, heatless solutes recovery by means ofchemical potential dissimilarity of solutions, as well as fractionationof gases based on the kinematic diameters of molecules, employing seriesof semipermeable flat membrane cells operating in symbiotic fashion,where each process is formed of closed hydraulic loops operating withina concentration potential field.

In regard to osmosis, this invention particularly promotes the design ofLarge Scale Renewable Resources (LSRR) anywhere natural or manmadephysical domains or ecological topography allows for cycling of watersof dissimilar salt concentration, preferably viaaccumulation-evaporation by natural renewable resources. This inventionallows for generating power from world endorheic (dead ended) salinewater, salt deposits, saline aquifers, dry salt lakes, formulatedionizable Inorganic salt solutions, as well as with a fully closed ISOsystems relying essentially on daily solar heat cycle.

Semipermeable membranes are effective and economical process for waterpurification or desalination by osmosis. However, current semipermeablemembranes technologies, particularly for seawater (3.5% salinity)desalination are limited to two types of commercial designs; spiralwound of flat sheet membrane and hollow fiber membrane, where the latertype membrane is monopolized by only one Japanese company. Regardless,the inventor offers several other technologies and applications thatemploy the currently manufactured flat sheet membrane. However, theseflat membranes have to be structured, assembled and operated asrectangular frames of multi-panels or leaves to meet the inventor'svision for developing several new water and gases novel applications.

this invention pertains to Permeable and Semipermeable Flat SheetMembranes (FSM) novel applications such as:

1. Agitated Axial Flow Reverse Osmosis,

2. Agitated Oscillating Flow Reverse Osmosis,

3. Agitated Axial Flow Vertical Wells Reverse Osmosis,

4. Agitated Axial Flow Underground Vertical Wells Reverse Osmosis,

5. Induced Symbiotic Osmatic [ISO] For Salinity Power Generation,

6. Symbiotic Hypersaline Water Reverse Osmosis,

7. Induced Symbiotic Osmosis (ISO) For Solutes Recovery/FluidsConcentration,

8. Symbiotic Gases Fractionation Processes.

Definitions of Claimed Invention

In aqueous solution, osmosis is the spontaneous movement of water,through a semipermeable membrane that is permeable to water butimpermeable to solute, where water moves from a solution in which soluteis less concentrated to a solution in which solute is more concentrated.

the driving force of the flow movement is the difference in the chemicalpotential on the two sides of the semipermeable membrane, with thesolvent moving from a region of higher potential (generally a lowersolute concentration) to the region of lower potential (generally highersolute concentration).

“Chemical Potential” appears to be an ambiguous and elusive terminology.In fact, it is one of the most important partial molar quantities. It isthe energy potential associated with the activity of the ions of anionizable substance. It is equal to the rate of change of system's freeenergy, known as “Gibbs Free Energy”, of a system containing a number ofmoles of such substance, when all other system parameters; temperature,pressure and other components are held constant. Simply, chemicalpotential is a form of energy like other kinds of potential; electrical,gravitational, momentum, magnetic, surface tension, etc. where, it isspontaneous and in the direction from high to low.

the difference in chemical potential of a substance in two adjacentphases separated by a semipermeable membrane determines the direction inwhich the substance diffuses spontaneously. When the components of amixture have the same chemical potential no chemical transport orreaction takes place, and no mutual diffusion will occur, because thereis no driving force. The chemical potential is an intensive property ofa substance in a phase.

to prevent this movement of water across the semipermeable membrane, apressure has to be imposed to equalize the force created by thedifference in the chemical potential of the solution across saidmembrane. This force is named osmotic pressure. If the imposed pressureexceeds this limit, then water begins to flow from the region of highersolute concentration to the region of lower solute concentration. Inthis case, the force is named reverse osmosis pressure.

regarding the title of this invention, the inventor believes thatosmosis is nature's one of the two gifts to life; Photosynthesis andOsmosis. It is the vehicle to transport fluids in all living cells andwithout it, all biological functions and all forms of life cease toexist! This phenomenon is attracting the attention of researchers as ameans to generate power. They tend to describe it in industrial termssuch as forward osmosis, ordinary osmosis, direct osmosis, pressureretarded osmosis, etc.

In order to harness this natural phenomenon, the inventor believes thatrelevant potential fields should be established to induce and bringabout the wonders of this phenomenon. Therefore, the inventor prefers todescribe all applications that utilize the power of osmosis for thebenefit of mankind as “Induced Osmosis”.

Further, the term “Symbiosis” although a biological phenomenon, itsgeneric or metaphorical concept refers to a mutually relationship ofcyclic reverberation, without altering or modifying any of the specificcomponents of the involved systems. In industrial applications,symbiosis is a process whereby a waste or less valuable byproduct in oneindustry is turned into a resource for use in one or more otherindustries. In essence, Symbiosis is the process of optimizing functionsof interrelated systems and achieves their ultimate availability.

Therefore, the inventor is naming the process of using osmosis totransfer water spontaneously from low salinity water to high salinitywater across a membrane in interrelated sequence of cells as “InducedSymbiotic Osmosis” and is abbreviated here by the acronym “ISO”.

DETAILED DESCRIPTION OF THE INVENTION

the proposed technology introduces rather new unique approach todesalinate or recover energy from hyper saline waters and entitled“Induced Symbiotic Osmosis Process [ISO]”. ISO comprises series ofcells, each forming a closed hydraulic loop comprising pumping and powerrecovery; generation turbine or pressure exchanger, sharingsemipermeable membranes between pre and post cells. Here, each cell ischarged with brine of specified salt quantity and type, operated atprogressively increasing concentration and osmotic pressure ratio, allcells in the series function simultaneously in symbiotic mode. Transportwithin cells is chemically driven under the influence of concentrationpotential field bounded by water of low salt concentration (LC) and bynatural or manmade brine of high salt concentration (HC),thermodynamically approaching reversibility between cells.

this invention is rooted in the field of physics and pertains to thedevelopment of a chemical engineering conceptual process design,presenting new vision in the energy field. The inventor believes thatunderstanding the basic physics and thermodynamics pertain to solutionsand osmosis and their industrial application in this alternative greenenergy field have comprehensive value in appreciating this proposedtechnology. Therefore, it is the objective of the inventor to presenthis vision in concise, simple presentation and easy to followexplanation of the subject process, without entanglement in equipmentand parts numbers. Further, all operating conditions and units ofmeasurement and analyses are clearly defined and stated to avoidcontroversial opinions when relevant arts are examined. This applicationis rather large and it is the intention to describe it in logical stepsstarting with theoretical and mathematical background, substantiatedwith examples and analytical evaluation, then followed by several largescale potential applications of different complexity.

the first law of thermodynamics rules out the possibility ofconstructing a machine that can spontaneously create energy. However, itplaces no restrictions on the possibility of transferring energy fromone form into another.

Then, osmotic pressure mathematical general form can be presented as:

Δπ=Δp=RTΔC _(s)  (Eq. 01)

The osmotic pressure it was originally proposed by Nobel Laureate Van'tHoff and modified to include Staverman's osmotic reflection coefficientto become;

π=ΦicRT  (Eq. 02)

Where:

π=osmotic pressure or force imposed on the membrane given in bars, atm,psi, etc.Φ=Osmotic Reflection Coefficient (NaCl=0.93, CaCl²=0.86, Mg CaCl²=0.89,etc.),i=Ions concentration per dissociated solute molecule (Na⁺ and Cl⁻ions=2),c=molar concentration of the salt ions,R=gas constant (0.08314472 liter bar/(k·mol)),T=ambient temperature in absolute Kelvin degrees (20° C.+273°=293° K).

In the case of sea water, the amount of average concentration of oceanssalt is about 3.5% (35 gram/liter) mostly in the form of sodium chloride(NaCl). For simplicity of calculation, it is assumed that seawatercontains 35 grams NaCl/liter. The atomic weight of sodium is 23 grams,and of chlorine is 35.5 grams, so the molecular weight of NaCl is 58.5grams. The number of NaCl moles in seawater is 35/58.5=0.598 mol/literand the osmotic pressure of seawater is

π=[0.93][2][0.598 mol/liter][0.08314 liter·bar/(k·mol)][293 K]=27.11 bar

Since one bar=100,000 Pascal (Pa) and one kilogram (force) per squarecentimeter (kg_(f)/cm²)=98066.5 Pascal, computation of osmotic pressure,π and energy, SW_(E), LW_(E) can be presented in several forms:

π=[27.1×10⁵ Pa]/[98066.5 Pa/(kg_(f)/cm²)]=27.63 kg_(f)/cm²

π=[27.63 kg_(f)/cm²][m/100 cm][1000 cm³/liter]=276.3 kg_(f)·m/liter

SW _(E)=[276.3 kg_(f)·m/liter][9.80665 Joule/kg_(f)·m]=2711Joule/liter=2.711 MJ/m³  a.

SW _(E)=[2711 Joule/liter][1 cal/4.184 J][1 kcal/1000 cal]=0.6479kcal/liter  b.

SW _(E)=[2711 Joule/liter][1000 liter/m³]=2.710 MJ/m³=0.751 kWh/m³  c.

In case of generating power continuously (1 m³ per sec, every second perday), which is the case with power generation systems, the theoreticalpotential power capacity of this system is:

[2.711 MJ/m³][1 m³/s][3600 s]=9.759×10⁹J=[9.759×10⁹ W·s][h/3600 s]=2,711kWh  d.

SW _(E)=[2,711 kWh][24 hrs/day][365 days/year]=23.75×10⁶ kWhannually.  e.

In the case of hyper saline lake such as in Gunnison Bay of the GreatSalt Lake-USA, the amount of average salt concentration is about 24%(240 gram/liter) mostly in the form of sodium chloride (NaCl). Lakewater osmotic pressure is calculated as:

π=[0.93][2][4.1026 mol/liter][0.08314 liter·bar/(k·mol)]·[293 K]=185.88bar

For continuous power generation by exchanging Gunnison Bay brine withBear River fresh water, at a rate of 1 m³ per sec, the theoreticalpotential power capacity of the lake water (LW) of such system where; 1W=J/s, 1 W·s=J, 1 kWh=3.6×10⁶ J, then:

LW _(E)=[18.2286 MJ/m³][1 m³/s][3600 s]=[65.623×10⁹J][1kWh/3.6×10⁶J]=18,228.6 kWh

LW _(E)=[18,228.6 kWh][24 hrs/day][365 days/year]=159.682×10⁶ kWh/year.

For membrane selection in osmotic processes, several types ofsemipermeable membranes such as stirred cell membrane, flat sheettangential flow membrane, tubular membrane, spiral-wound membrane andhollow fiber membrane can be used for the ISO technology applications.In this invention, high pressures Semipermeable Flat Sheet Membranes(SFSM) that are intended for seawater and brine desalination are beingadopted. Such membranes should operate with salinity that is less thansalt saturation point to minimize concentration polarization, as well asmaintaining relatively even flow distribution through the flat membranepanels.

Commercially available permeable and semipermeable flat sheet membraneelements of conventional sizes (generally 40 inch×60 inch, ˜1.0 m×1.5m), or commercially available suitable membrane of other sizes are beingadopted in this invention for water filtration, gases fractionation,

brackish water and seawater desalination, fluid extraction and soluterecovery, symbiotic salinity power generation, symbiotic Hypersalinityreverse osmosis, where flat sheet membrane elements are adapted for useas flat plates in the form of rectangular panels, mounted in rectangularframes comprising top and bottom water collecting headers, where saidframes assembly is mounted within one or more sequential or parallelpressure vessels.

In case of water desalination, the membrane elements are subjectedexternally to pressurized untreated water at a pumping pressure that ishigher than its osmotic pressure, as in case of reverse osmosis, wheretreated water is collected in the frame headers and transported tostorage for future use, while the rejected saline water outside themembrane is disposed.

In case of osmotic power generation, the membrane elements are subjectedexternally to saline water operating at a pumping pressure that it isrelatively less than its osmotic pressure, to enhance treated low or nosalinity water flowing in the frame headers to be induced spontaneouslyacross the flat semipermeable membrane into the saline water, where thecombined flows of both the saline water and the permeated induced water,being at the initial saline water pumping pressure, is circulatedthrough a turbine to generate power that exceeds the power that isconsumed to pump the saline water. The same cycle is repeated in thesubsequent cells, but at different concentrations and pumping pressures.

The subject technology is adaptable to the various specifications offlat sheets membranes and is a companion technology to the inventor'sU.S. Pat. No. 8,974,668 for hollow fiber applications.

Concentration polarization results of accumulation of dissolved salt atthe membrane surface, creating relatively high localized osmoticgradient, reducing osmotically driven normal permeate diffusion andhinders membrane flux. However, since ISO cells are charged withcirculated brine of formulated salt content in closed loops, membranesare less susceptible to concentration polarization. Pretreatment isrequired for inlet water feed, particularly when organic fouling isanticipated. In general, membranes operating in induced osmosis mode areless susceptible to this phenomenon due to the low pressure imposed onmembrane as compared with membranes in reverse osmosis service.

Energy, as equated to the water head, of this stream is now higher thanthe potential energy of the seawater feed, where it is preferentiallyused to generate energy.

Symbiotic Osmosis Power Generation is a grassroots technology.Inventor's U.S. Pat. No. 8,545,701 should be consulted in any attempt toevaluate the potential of the various domains. Since the objective hereis to generate power, each system must be analyzed based on equitableand technically sound criterion to determine validity of assumptions andmerits of such processes. Therefore, several parameters and means ofmeasurements are defined by the inventor in the following to facilitatesystems simulation:

Specific gravity, SG is estimated at 20° C., using the inventor'sfollowing relation:

[SG=1+0.0077×C %],

where C is salt concentration in the form of sodium chloride, sincesaline waters contain mostly this salt.

Turbine Energy (MJ)=(η)(ρ)(g)(h)(Q),

where η: turbine efficiency (<1.0), ρ: density (kg/m³), g: accelerationof gravity (9.81 m/s²), h: water column height, head (m), Q: water orbrine flow (m³/s), MJ: Mega Joule, Watt=Joule (J)/second.

Another simplified estimation is based on concentration, where turbinegenerated power equals [(0.658 MJ per 1% of concentration) (C %) (SG)(Q)], based on turbine hydraulic efficiency of 85% and where C, SG and Qare flow conditions at the turbine inlet.

Similarly, pumping requirement can be also based on concentration, wherepump shaft energy equals [(1.033 MJ per 1% of concentration) (C %) (SG)(Q)], based on pump efficiency of 75% and where SG and Q are flowconditions at the outlet of the pump, but C is the concentration % atthe inlet of the turbine, where pumping is intended to overcome theosmotic pressure leaving the membrane.

Considering as an example the power generation from the Great Salt Lakeof Utah, USA, an ISO train comprises three (3) cells operating atconstant cell (HC/LC) ratio of 4.0, employing 1 m³/s from Gunnison Baywith salinity of 24% salt is exchanged with 3 m³/s with negligiblesalinity from Bear River water, operating at equal Log Meanconcentration difference (LMCD) of 4.43 across membranes would generatea net energy of about 17,000 kWh.

Fouling of membranes is a serious problem in reverse osmosisdesalination and directly affect process efficiency and economics. PallCorporation indicated that 28% Costs Improvement can be achieved byeffectively protecting reverse osmosis units. Generally all types ofmembrane separation technology are susceptive to a certain degree offoiling. In principal, reverse osmosis is a process is intended tofilter water only. Since water molecules is about 0.275 nanometer(0.275×10⁻⁹ meter), then any particle larger that this size isconsidered a foiled matter and has to be removed.

However, since there are different types of foiling, different types oftreatment may be required; i.e., mineral deposits, organic and inorganicmatter, biological matter, bacterial and algae films, dissolved chemicalcompounds, herbicides and insecticides, etc., it must be more than oneprocess to remove these foreign matter before any reverse osmosisprocess.

In addition, there are also other significant types of foiling thattakes place within and among the membranes surface.

Concentration Polarization is one type of these foiling mechanism thatresult in formation of salt spots or layers on the membrane surface thathave higher salt concentration, increasing the osmotic pressure at themembrane surface than the feed water and causing reversed is the flowdirection, reducing the separation efficiency of this membrane. For thisreason, the inventor specify, in all his membrane separationtechnologies, that membrane contact is not allowed and flow velocity ismaintained at minimum Reynolds Number of 3000. Regarding fluxredistribution in multi-elements reverse osmosis system, housing has tobe sized to meet Reynolds number criterion. Where Reynolds number iscalculated as follows:

Re=(ρvD _(H))/μ

ρ=density(kg/m³),v=velocity(m/s),D _(H)=hydraulic diameter,

μ=Dynamic viscosity kg/(m·s)

Existing technologies suffer from what is known as concentrationpolarization phenomenon. The use of hydrophilic semipermeable membranesin hollow fiber panels significantly mitigates this phenomenon.Hydrophilic literally means “water-loving.” Accordingly, a hydrophilicmaterial exhibits an affinity for water, and tends to readily adsorbwater.

Suitable hydrophilic semipermeable membranes have a surface tensionsufficiently high (surface tension of the membrane has to be higher thanthe surface tension of water) to maintain materials at the surface ofthe semipermeable membrane in liquid form. In one embodiment, thesurface tension of the hydrophilic semipermeable membrane is about 35dyne/cm or more.

In one embodiment, the hydrophilic semipermeable membrane material has asurface tension of about 44 dyne per centimeter or more. Hydrophilicmembrane materials having suitable surface tensions include, forexamples, Polyepichlorohydrin (surface tension-35), Polyvinyl Chloride(PVC) (surface tension-39), Polyethersulfone (surface tension-41),Polyethylene Terephthalate (Polyester) (surface tension-43),Polyacrylonitrile (surface tension-44); Cellulose (surface tension-44),and variants thereof.

in one embodiment, the hydrophilic semipermeable membrane material iscellulose acetate. Cellulose acetate has a surface tension of 44 dyneper centimeter (dyne/cm), or 44 milli Newton/meter. In one embodiment,the hydrophilic semipermeable membrane is a cellulose triacetate (CTA)membrane. A suitable CTA seawater semipermeable membrane in the form ofhollow fiber is manufactured by the Japanese corporation, Toyobo Co,Ltd, In one embodiment, a flat sheet membrane Zirfon manufactured byAgfa for alkaline waters.

the present invention may be subject to many modifications and changeswithout departing from the spirit or essential characteristics thereof.The present embodiment should therefore be considered in all respects asillustrative and not restrictive of the scope of the subject inventionas defined by the appended claims.

Revise Osmosis Membranes by Some Manufacturers

Membrane Polyamide Feed Type Flux (gfd/psi) NaCl Rejection Toray 82V SeaLow Energy/High Rejection 27/798 99.73% DOW SW30HR Sea High Rejection17-24/800   99.60% DOW BW30 Brackish Standard 26/255 99.50% DOW BW30FRBrackish Fouling Resistant 26/255 99.50% DOW SW30XLE Sea Extra LowEnergy 23-29/800   99.50% GE AD Sea High Rejection 15/800 99.50% GE AGBrackish Reactive Si Removal 26/225 99.50% TriSep ACM1 Brackish Tight25/225 99.50% TriSep ACM2 Brackish Standard 30/225 99.50% Toray 72UBrackish Extra Low Pressure 29.5/109   99.40% TriSep ACM3 Brackish LowPressure 35/225 99.30% TriSep ACM4 Brackish High Flux/Low Pressure30/150 99.20% DOW BW30LE Brackish Low Energy 37-46/225   99.00% GE AKBrackish Low Energy 26/115 99.00% Toray 70HA Brackish Extra Low Energy23.3/73   99.00%

Apparatus Relevant Components, Design and Specification List:

FIG. 01: Prior Art-Applicant Patented High Capacity Hollow Fiber [HFM]Frame Design,

FIG. 02: Flat RO panels assembly,

FIG. 03: Flat RO panels frame,

FIG. 04: Flat Reverse Osmosis Membrane Frame,

FIG. 05: Type 1 Simple Frame Layout for small vessels-single sizemembranes Occupies ˜64% of the vessel's Section,

FIG. 06: Type 2 Frame layout two membrane sizes,

FIG. 07: Type 3 Frame layout large exchange surface, but multiplemembrane sizes,

FIG. 08: Top Cross section of a flat RO membrane panel parts andassembled unit

FIG. 09: Vertical cross-section in a frame comprising a stack of 6-12flat RO membrane panels of FIG. 8,

FIG. 10: Desalinated water frame headers and desalinated watercollection header (top & bottom),

FIG. 11: Vertical cross-section of two connected frames each comprisinga stack of 6-12 flat RO membrane panels (leaves),

FIG. 12: Stack of Flat Reverse Osmosis Membrane Panels' Top CrossSection,

FIG. 13: Flat Reverse Osmosis Membrane Frame for multiple panels(leaves),

FIG. 14: Flat RO Membrane Rectangular Frame of One or More MembranePanel (leaf),

FIG. 15: Stack comprising 6-8 rectangular frames of flat reverse osmosismembranes, mounted in cylindrical pressure vessel. Each frame holds 6-12RO panels (leaves). RO Panels varies from about 250 mm (˜10 inch)-1.00 m(˜40 inch) in width and 250 mm-2,000 mm (˜10-40 inch) in length, orhigher,

FIG. 16: RO membrane stacked frames in a horizontal pressurizedcylindrical housing vessel,

FIG. 17: Side Cross Section of a Twin RO Staked Sequential orIndependent Desalination Frames,

FIG. 18: Agitated Axial Flat Sheet Membranes (FSM) Variable Flow ReverseOsmosis Scheme,

FIG. 19: Indoor or Outdoor Mounting RO Enclosure Vessels Each TrainComprises 2-6 Sequential Compartments,

FIG. 20: Cross Section Top View in Vessel Well Reverse Osmosis Type IMembrane,

FIG. 21: Axial Flow Vertical Well Reverse Osmosis—Flat Membrane Type1,

FIG. 22: Membrane Frames Multi-Compartments Type 2 Assembly,

FIG. 23: Enclosures (cages) for Membrane Frames Multi-Compartments Type2 Assembly,

FIG. 24: Single Compartment Type 2 Membrane Frames Assembly,

FIG. 25: Single Compartment Type 2 Membrane Frames' enclosure (cage),

FIG. 26: Single or multiple stages for filtration and desalinationtowers or vertical wells. Axial flow [FSM] applicable design for macro,micro, ultra and nano filtration, as well as applicant's osmotic powergeneration and salinity reverse osmosis employing Type 1, 2 and 3membrane processes.

1-20. (canceled)
 21. Methods of Making Flat Sheet Membrane [FSM]Apparatus Adapted for various symbiotic fluids fractionation and osmoticprocesses in this application comprising three distinctive methodologiesfor fabricating and mounting conventional permeable or semipermeablemembrane sheet in the form of plurality a spaced apart, self-supportedand un-rolled spiral wound configuration membrane flat surface panel(leaf), essentially employing same conventional permeable orsemipermeable membrane sheets. 21a. The first methodology whereinadjacent permeable or semipermeable membrane flat sheets, in anun-rolled configuration, is formed by two adjacent permeable orsemipermeable membrane flat sheets of same size and specifications,separated by flat porous permeate carrier, in the form of a hard board,comprising intermediate flow channels or permeable inert structure forcommunicating permeated desalinated water across said flat sheetmembranes, in a horizontal pattern to the vertical side headers of aflat sheet membrane panels frame, as in case of vertically mountedenclosing vessels (FIG. 4), wherein each of the opposite membrane paneledges, top and bottom, are heat or epoxy sealed. Such flow patternarrangement is reversed when vessels are mounted horizontally. Saidprocess can be automated by laying the first permeable or semipermeablemembrane flat sheet on a moving belt, followed by laying the flat hardboard porous permeate carrier on to top of the first membrane sheet,then followed by laying the second permeable or semipermeable membraneflat sheet and finally seem welding the top and bottom membrane sheetswith epoxy material or heat. 21b. The second methodology comprisingreplacement of the two membrane sheets of claim 21a, by permeable orsemipermeable membrane films that can be formed as a tube, either byemploying blown-film extrusion process of molten and malleable resinpellets, in a similar fashion for forming conventional plastic bags, ifmembrane physical and chemical specifications are adaptable for suchprocess, or by mechanically rolled the required membrane sheet in a tubeform and seal its edges. In either application, the circumference ofsaid tube has to be completely and securely overlay the flat porouspermeate carrier board. This implies the need to heat the membranepolymeric tube with hot dry air or nitrogen @ 40-45° C. in a heatingchamber, if tube has already been formed in a roll. Then flatten the endof the malleable formed tube, while it is hot, and slide it on the flatporous permeate carrier board, which can be accomplished, preferably byusing automatic bag filling and sealing machine (modified version ofzipper bags filling/sealing) to open the end of the extruded polymerictube by air suction to expand tube diameter by few millimeters, theninserted on the flat porous permeate carrier boards being mounted on amoving conveyor belt. As the film cools, it shrinks maintaining secureflat sheet film on both side of porous permeate carrier board. Then, theprocess is completed but cutting/trimming the required flat sheetmembrane length for mounting in the desalinated water header of themembranes frame. This process is more suited for vertically mounted flatporous permeate carrier board assembly lines. For an example, a membranetube 19 cm (7.5 inch) in diameter overlays both sides of a flat membranepanel of 30 cm (11.8 inch) wide. 21c. The method further comprisingmodification of flat sheet membrane of claim 21, where a plurality ofspaced apart, self-supported, vertically mounted flat sheet membranepanels assembly, wherein adjacent permeable or semipermeable membraneflat sheets, in an un-rolled configuration, can be formed efficientlyand economically by laying down the selected membrane film, of asufficient width on a speed-controlled moving belt(s) of several meterslong, to securely wrapping both sides of the permeate carrier board,then laying down the flat porous permeate carrier board for the fulllength of the belt, then automatically wrapped the two sheet edgesfairly tight around the board and seal these edges by adhesive sealing,heat sealing, or ultrasonic welding, where the sealing process isfollowed by an automatic process to cut this long film assembly to therequired Flat Sheet Membrane panel (leaf) length. The process is mostsuited for narrow and square membrane panels (leaves), where themembrane outlets width of the desalinated water discharge is at orlonger than the panels' sealed sides.
 22. Wherein the panel surface istightly wrapped by a highly porous protective woven fabric, secured byepoxy sealed sleeves, or equivalent means, at the panel both side ends,then the panel is shielded with protective rigid polymeric or rustproofmetallic porous screen.
 25. Wherein a stack of plurality of uniformmembrane panels are mounted within detachable top and bottom of holdingcaps that can be securely inserted and epoxy scaled to the top andbottom headers of the flat sheet membrane frame for communicatingtreated water.
 26. Wherein said mounted membrane panels are separatedapart to maintain flow Reynold's number of 3,000-3,500 for mitigatingmembrane fouling, while maintaining=a minimum clearance of least of 1.0mm (˜0.04 inch) for regular membranes maintenance procedures. 27.Wherein said flat sheet membrane panels [FSM] for osmotic processes areexceptionally large in size than that of conventional desalinationmembranes and uniquely designed for operating at pressures of up to 70kg/cm² (1,000 psi), would be mounted in frames of up to one meter inwidth and more than two (2) meters in length, or more;
 28. Wherein, flatsheet membrane panel's frames, of essentially same configuration, but ofvarying specification and operating conditions are housed in largeholding compartments of essentially cubical shapes that are mountedwithin a vertical tower or horizontal train of sequential set ofvessels, for specific process applications; macro filtration, microfiltration, ultra-filtration, nano filtration and reverse osmosis. 29.Wherein flat sheet membrane in the form of polymeric sheets or ceramicsheets, as well as in the form of hollow fiber can be mounted inindependent vessels within the same desalination and salinity powergeneration trains of multi vessels.
 30. Wherein, flat sheet membranepanel [FSM] frames, of essentially the same configuration, but ofvarying specification and operating conditions are housed in vertical,single stage axial flow pressure vessels, mounted above or for belowgrade, or housed in multi stages water desalination towers (U.S. patentapplication Ser. No. 14/967,295),
 31. Wherein, the water desalination orbrine power generation operating capacity determines the size, weightand the mechanical integrity of equipment; where size and number ofpanels is dictated by availability of safe means to handle, operate andmaintain such operating systems;
 32. Wherein, small desalinationoperating capacity that may require 15 membrane panels, with frameheader cross section of 20 cm, only one single frame of 20 cm size canbe used considering the relatively light weight of the frame and itsmounted panels.
 33. Wherein, the large operating desalination capacitythat may require multiple heavy weight frames, then the membrane panelsframe header can be 10-15 cm (˜4-6 inch) in width, comprising 6-12membrane panels; where size and number of panels is dictated by waterflow rates, turbidity and salinity, availability of safe means tohandle, operate and maintain such operating systems;
 34. The method ofclaim 21 further comprises: A plurality of spaced apart, verticallymounted flat ceramic membrane panels assembly, wherein adjacentpermeable membrane flat sheets can be used ahead of the semipermeablereverse osmosis polymeric flat sheet membranes [FSM], for waterfiltration and can be formed, as well, by separating these panels withflat porous permeate carrier comprising an intermediate flow channelsfor communicating permeated filtered water across said flat ceramicmembranes, Wherein, said ceramic membranes are mostly suitable formacro, micro and ultrafiltration, generally has limited operatingpressure of about 300 psi, but less sensitive to temperature changes,35. The method of claim 21, 22, 23, further comprises: Automated orsemi-automated assembly platform (assembly line) for assembling flatsheet membrane panels in sequential steps, comprising a moving belt,where the first shielding screen is laid down on the belt, followed by afeed spacer, then by a flat membrane panel, followed by a feed spacer,then by the second shielding screen, where bottom and top shieldingmetallic screens edges are continuously welded or epoxy sealed, ifscreens are of polymeric materials, where this automated process forpanel's assembly could potentially construct 90-120 panels per hour. 36.The methods of claim 21, 22, 23 through claim 35 further comprising:Means for measuring fluid properties; flow rate, temperature, density,viscosity, acidity, radioactivity, etc., as well fluid sampling, flowconditioning and property adjustment for various processes. Where saidFlat Sheet Membrane [FSM] apparatus is capable of processing severalfluids, including: seawater and brines reverse osmosis desalination andosmotic power generation, flowback and produced water fractionation inthe hydraulic fracturing process, in-situ leaching of undergroundsoluble minerals, fractionation of alcohols mixtures, removingradioactive from water, medical solutions, fractionation of industrialgases,
 37. Flat porous permeate media in claims 21, 22, 23 can be madeof Polysulfone membrane support boards, less than 5 micron pores,Zirfon® with low zirconia. Also, interstitial porous aluminum oxide,woven metal screen, channels or nonwoven polyester or Polysulfone fibermat. Epoxy sealing sleeve for right & left edges of vertically mountedmembrane panels,
 38. Feed Spacer can be made of Polyester orpolypropylene, or comparable material;
 39. Seawater, brackish water andbrines desalination membranes are made of polyamide or cellulose acetateflat sheets, or comparable material;
 40. The methods of claim 36 furthercomprising: Means for adjusting fluid temperature to sustain membranemechanical integrity and fluid separation or retention of solutes, wherethe change of fluid temperature, as a result of atmospheric weatherchanges; summer and winter, on open water domains operation, can haveserious implication on polymeric membrane pore size. This function isvery important in the development of “Ecologically Sustainable HydraulicFracturing [ES-FRAC] Process” by the same applicant of the currentpatent application!
 41. A frame configured to house the plurality of thecaped (Please see FIG. 2) membrane Panels; the frame includes: a topheader in communication with the first end cap and a bottom header incommunication with the second end cap, each end cap configured to restwithin a track formed in the bottom and top headers; a side memberhaving a porous surface configured to permit the passage of saline water(or other saline fluids); and an outlet formed in at least one of thetop header and the bottom header to allow passage of desalinated water(or other Fluids); wherein pressurized saline water is forced to passedthrough the porous side member of the frame through the flat sheetmembranes.
 42. The panel assembly of claim 21, 22, 23, 36, wherein theplurality of flat sheet membranes is configured to be suitable for atleast one of filtration or fractionation function; brackish water,seawater, brines desalination, fluid extraction, solute recovery,symbiotic salinity power generation, symbiotic Hypersalinity reverseosmosis, and gas mixture fractionation.
 43. The panel assembly of claim21, 22, 23, wherein the plurality of flat sheet membranes is adapted foruse in a rectangular shape.
 42. The panel assembly of claim 21, 22, 23,wherein treated water is collected through the plurality of headers andthe brine waste water is disposed of, or used as a source for salt, asin the case of seawater desalination.
 44. The panel assembly of claim21, 22, 23, wherein the plurality of the flat sheet membranes are madeof at least one of a polyamide and a cellulose acetate, or equivalentmembrane material, having a pore size suitable for filtration ordesalination.
 45. The panel assembly of claim 21, 22, 23, wherein theplurality of flat sheet membranes are separated by a permeate carrier.46. The panel assembly of claim 21, 22, 23, wherein the permeate carrieris configured to resist collapse under the operating pressure of thefluid.
 47. The panel assembly of claim 21, 22, 23, further comprising: ashielding screen coupled to a surface of the flat sheet membranes panelsand configured to protect membranes from damage.
 48. The panel assemblyof claim 1, wherein the frame is configured to include a rolling deviceconfigured to translate the frame on the bottom header within thepressure vessel.
 49. In all design cases, desalinated water collectingheader has to be on the long side of the membrane panels (leaves) toavoid restricting the flow of desalinated water through the membrane.50. This invention pertains to Permeable and Semipermeable Flat SheetMembranes (FSM) applicant's novel applications such as: a. Agitatedaxial and oscillating flow reverse osmosis, b. Agitated axial flowunderground vertical wells reverse osmosis, c. Induced symbiotic osmatic[ISOP] for salinity power generation, d. Symbiotic hypersaline waterreverse osmosis [SRO], e. Induced symbiotic osmosis [ISO] for solutesrecovery/fluids concentration, f. Symbiotic gases fractionationprocesses [SGF]. g. Ecologically sustainable hydraulic fracturingprocess [ES-FRAC].